CN104277859B - Separation method of Fischer-Tropsch reaction products - Google Patents
Separation method of Fischer-Tropsch reaction products Download PDFInfo
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- CN104277859B CN104277859B CN201310286088.3A CN201310286088A CN104277859B CN 104277859 B CN104277859 B CN 104277859B CN 201310286088 A CN201310286088 A CN 201310286088A CN 104277859 B CN104277859 B CN 104277859B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
- C10G7/12—Controlling or regulating
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1022—Fischer-Tropsch products
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a separation method of Fischer-Tropsch reaction products so as to mainly solve the problem that it is difficult to separate present Fischer-Tropsch synthesis reaction products gasoline and diesel. According to the technical scheme, hydrocarbon products obtained after a Fischer-Tropsch reaction are injected into a separator; the products are separated by the separator to obtain hydrocarbon and heavy hydrocarbon products containing gasoline and diesel; the separator contains a heat sink tower and a heater; the heater is arranged below the heat sink tower; temperature at the bottom of the heat sink tower is controlled within the range of 120-400 DEG C; and temperature at the top of the heat sink tower is controlled within the range of 25-150 DEG C. By the technical scheme, the above problem is solved well. The separation method can be used in industrial production for separation of Fischer-Tropsch reaction products.
Description
Technical field
The present invention relates to a kind of separation method of fischer-tropsch reaction product.
Background technology
Nineteen twenty-three, Germany scientist FranzFischer and HansTropsch use first ferrum-based catalyst by one
Carbonoxide and hydrogen are reacted, and synthesize the product based on oxygenatedchemicals and alkane.Hereafter, they have used cobalt-based again
Catalyst, obtains the product that almost all is n-alkane.Hereafter, in order to commemorate this discovery of two people, people are by carbon monoxide
There is the method that hydrogenation reaction generates different carbon number hydrocarbon compounds in the presence of high temperature, condition of high voltage and catalyst, claim
For F- T synthesis (Fischer-Tropsch Synthesis, referred to as FTS).
Fischer-Tropsch synthesis product composition is complicated, the relatively wide (C of carbon number distribution scope1～C50), wherein containing different carbon numbers
Positive structure, isomeric alkane (alkene) hydrocarbon and aromatic hydrocarbons.In fischer-tropsch catalysts laboratory evaluation development process, the complexity of hydrocarbon product species is more
Sample brings very big difficulty for its qualitative, quantitative analysis work.For example, (K. Snavely, the B. such as Snavely
Subramaniam, Automatic gas chromatographic retention time matching applied to
synthetic petroleum (Fischer-Tropsch) products, using HP Chemstation
Software, J. Chromatogr. A. 791 (1997) 197-202.) find it is difficult to qualitative by temperature programming index
The hydrocarbon product of different carbon numbers；And Westhuizen (R. V. Westhuizen, A. Crouch, P. Sandra, The
use of GC+GC with time-of-flight mass spectrometry to investigate dienes and
Diels–Alder polymerisation products in high-temperature Fischer–Tropsch-based
Fuels, J. Sep. Sci. 31 (2008) 3423-3428.) etc. and Bertoncini (F. Bertoncini, M.C.
Marion, N. Brodusch, S. Esnault, Unravelling Molecular Composition of
Products from Cobalt Catalysed Fischer-Tropsch Reaction by Comprehensive Gas
Chromatography: Methodology and Application, Oil Gas Sci. Technol. 64 (2009)
79-90.) bidimensional gas-chromatography off-line analysis liquid phase hydrocarbon product, simple sample analysis time etc. is used to be more than 70 minutes.
For the exploitation that fischer-tropsch reaction synthesizes vapour, diesel catalytic converter, in synthetic product in addition to vapour, diesel component, also
There is C1～C4Gas phase hydrocarbon and C18 +High-carbon hydrocarbon liquid phase.Generally, gas phase hydrocarbon and C5 +Liquid phase hydrocarbon product is respectively through a gas phase color
Spectrum carries out online, off-line analysis, and final comprehensive two chromatogram analysis datas could obtain evaluating catalyst result, chromatography
Journey is relatively complicated and time-consuming longer, particularly C5 +The carbochain of liquid phase hydrocarbon compound is longer, and its composition chromatography time gets over
It is long.
If separative element can be centered in F- T synthesis dress, by C5～C18Vapour, diesel oil target product are from C5 +Hydrocarbon liquid phase
Pre-separation in class product can out, then greatly shorten the chromatography time, so as to accelerate fischer-tropsch reaction synthesis vapour, diesel catalytic converter
Screening and development rate.
The content of the invention
The technical problem to be solved is existing Fischer-Tropsch synthesis product vapour, diesel oil separation difficulty, during separation
Between long problem, there is provided a kind of new separation method for fischer-tropsch reaction product, the separation method is used for into F- T synthesis anti-
When answering the separation of product vapour, diesel oil, with Fischer-Tropsch synthesis product vapour, diesel oil simple, the short advantage of disengaging time is separated.
To solve above-mentioned technical problem, the technical solution used in the present invention is as follows：
A kind of separation method of fischer-tropsch reaction product, by the hydrocarbon product that fischer-tropsch reaction is obtained separator is passed through；Product
Separated device is obtained containing vapour, the hydro carbons of diesel oil and heavy hydrocarbons product after separating, and the separator includes hot trap tower and heating
Device, in the bottom of hot trap tower, hot trap column bottom temperature control range is 120～400 DEG C to heater, hot trap tower top temperature control range
For 25～150 DEG C；
The hydrocarbon product that the fischer-tropsch reaction is obtained by percentage to the quality, including following components：15.1～19.5%
C1, 9.0～12.4% C2～C4, 65.0～50.0% C5～C11, 10.5～12.9% C12～C17, 0.4～4.7% C18~
C27, 0～0.5% C28 +。
In above-mentioned technical proposal, the hydrocarbon product for leaving fischer-tropsch reactor is entered directly in the hot trap tower through transforming；
Hydrocarbon product after the separation of hot trap tower, in ensuing cold-trap holding vessel collect, and can obtain by the target hydro carbons that tower top is obtained
To C5～C11Gasoline fraction or C5～C18Vapour, diesel oil mixed fraction；Hot trap bottom of towe sets up heater, leaves fischer-tropsch reactor
Hydrocarbon product is fed by tower middle part, and tower top is in atmospheric environment or arranges product condenser, and filler, charging aperture are set up in tower
The filler that upper and lower position is installed is located at 1/3rd and 2/3rds of hot trap tower；The preferred model of hot trap column bottom temperature control
Enclose for 120～400 DEG C, Optimal Temperature scope is 150～380 DEG C；The preferred scope that hot trap tower top temperature is controlled is 25～150
DEG C, Optimal Temperature scope is 25～80 DEG C；The hydrocarbon product for leaving hot trap enters directly into the cold-trap of another temperature control
In holding vessel, vapour, diesel oil hydrocarbon product are collected in the holding vessel, and its component can carry out offline chromatography.
The temperature controlled preferred scope of cold-trap holding vessel is -10～25 DEG C, and Optimal Temperature scope is -5～10 DEG C.
Synthesis gas through fischer-tropsch reactor reaction after, hydrocarbon product leave reactor enter into hot trap middle part, by hot trap by
Simple product storage transform a fractionating column or rectifying column pattern as, and wherein bottom of towe arranges heater, and tower top is in big
In compression ring border or product condenser is set, the temperature of tower top can individually control by heater, also can by heater with
Condenser is acted on simultaneously；Filler is set up in tower for increasing air-liquid contact area, so as to reach the mesh of separating hydrocarbons product carbon number
, described filler is the filler commonly used in industrial production, general inert solid material all can, such as Pall ring, Raschig ring, gold
Category silk screen etc..After the separation of hot trap tower, vapour that tower top is obtained, diesel oil target hydro carbons are stored hydrocarbon product in ensuing cold-trap
Offline chromatography is collected and carried out in tank；
Hot trap can transform fractionating column or the principle of rectifying column as：Using different carbon number hydrocarbon product relative volatilities
It is different and separated.
Vapour, diesel oil are mainly C5～C11And C12～C18Hydrocarbon mixture, the cutting of each carbon number component need not be very accurate,
As long as the temperature of the bottom of towe heater 3 of precise control hot trap 1, then can obtain the gasoline or vapour of separator well, diesel oil in tower top and mix
Close target hydrocarbon product.
Additionally, Fischer-Tropsch synthesis are typically carried out in the case where pressure is more than 1.0 MPa, hydrocarbon product bubble point is higher, hot trap tower
Filler is set at 1/3rd to increase air-liquid contact area.Axial temperature using hot trap is poor, realizes that tower top some hydrocarbon steams
Gas condensing reflux, air-liquid carries out mass transfer on filler surface, so that hydrocarbon product is separated；The tower top of hot trap 1 is in big
In compression ring border or arrange condenser 4, be conducive to the condensation of tower top hydrocarbon vapours；When charging aperture lower position installs filler 5,
Hot trap 1 is equivalent to rectifying column；In theory, as long as light component realizes part condensing reflux in tower top, it is possible to the hydro carbons for rising
Steam carries out gas, liquid mass transfer, reaches fractionation purpose.The present invention carries out flow process to the hydrocarbon product that specific fischer-tropsch reaction is obtained
Arrange, the control to hot trap column overhead temperatures and column bottom temperature in separator, separation achieves unforeseeable technique effect,
C5～C18Vapour, diesel oil distillate section disengaging time highest can shorten 50%.
Description of the drawings
Fig. 1 is Fischer-Tropsch synthesis product separator schematic diagram provided by the present invention.
Fig. 2 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 1.
Fig. 3 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 2.
Fig. 4 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 3.
Fig. 5 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 4.
Fig. 6 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 5.
Fig. 7 is 93#Gasoline chromatogram.
Fig. 8 is 97#Gasoline chromatogram.
Fig. 9 is hydrocarbon product chromatogram in the cold-trap 2 of embodiment 6.
Figure 10 is hydrocarbon product chromatogram in the hot trap 1 of comparative example 1.
Figure 11 is hydrocarbon product chromatogram in the cold-trap 2 of comparative example 1.
As shown in figure 1, hydrocarbon product is left by the charging of the middle part of hot trap 1 after fischer-tropsch reactor, hot trap bottom arranges heater
3, top is in atmospheric environment or arranges condenser 4, and hot trap tower is interior to arrange filler 5 and 6；The control bottom of towe heater 3 of hot trap 1
Temperature, by tower reactor hydrocarbon product partial gasification, the liquid hydrocarbon product for rising decline at steam and charging aperture enters on the surface of filler 5
Promoting the circulation of qi, mass transfer in liquid phase；And the steam that charge door top rises is being filled out with the withdrawing fluid under atmospheric environment or condenser condensation
Expect that 6 surfaces carry out gas, liquid mass transfer；Next product enters the middle part of cold-trap 2 with cooler 7, is stored by controlling cold-trap 2
The temperature of tank is allowed to condense, and in the bottom of cold-trap 2 gasoline or vapour, diesel oil compound target hydrocarbon product can be collected, and hot trap 1
Bottom of towe will obtain heavier C18 +Hydrocarbon product, and can periodically discharge.
Specific embodiment
【Embodiment 1】
Hydrogen and carbon monoxide are with mol ratio 2 to 1 into the fixed-bed micro-reactor that internal diameter is 8 millimeters, reactor middle part
Admission space is 3 milliliters of cobalt-base catalyst, synthesis gas reaction pressure be 2.0 MPa, temperature be 250 DEG C, air speed be 1000
h -1Under the conditions of reacted.After reaction carries out stablizing for 24 hours, hot trap 1 and cold-trap 2 are only as holding vessel, room temperature timed collection
And hydrocarbon liquid phase composition therein, comprehensive gas phase hydrocarbon analyze data are analyzed, the hydrocarbon product Mass Distribution for obtaining is：C1 =
15.1%, C2～C4=9.0%, C5～C11=65.0%, C12～C17 =10.5%, C18～C27 =0.4%, C28 + =0。
After Fischer-Tropsch synthesis are stable, the hydrocarbon product with above-mentioned Mass Distribution leaves after reactor and is into internal diameter
15 millimeters, a length of 30 centimetres of the middle part of hot trap 1, bottom of towe arranges heater, 8 centimetres of heater height, and temperature control is 150 DEG C,
Tower top arranges condenser, and temperature control is 100 DEG C, on charging top, 8 centimeter length stainless steels gold is filled at the position of tower 1/3rd
Belong to silk screen to increase the contact area between the steam of rising and the condensing reflux liquid of decline, so as to strengthen the mass transfer between the two.
The tower top outlet gas of hot trap 1 is entered with the holding vessel of temperature controlled cold-trap 2 middle part, and the temperature control of cold-trap 2 is 10 DEG C.
The liquid phase hydro carbons product quality that hot trap 1 and the cummulative metering of cold-trap 2 are generated, accumulated time is 5 hours, the liquid phase for obtaining
Hydrocarbon carries out respectively chromatogram off-line analysis, calculates the weight/mass percentage composition of different carbon number hydrocarbon products.Now, product color in hot trap 1
The analysis of spectrum time is 78 minutes, and product focuses primarily upon C in cold-trap 25～C18Vapour, diesel oil distillate section, the chromatography time is
60 minutes, chromatogram was as shown in Fig. 2 data result is as shown in table 1.
【Embodiment 2】
Using Fischer-Tropsch synthesis condition same as Example 1, simply change catalyst and cause hydrocarbon product quality point
Cloth is：C1 =19.5%, C2～C4=12.4%, C5～C11=50.0%, C12～C17 =12.9%, C18～C27 =4.7%, C28 +
=0.5%。
The bottom of towe heter temperature of hot trap 1 is set to into 150 DEG C, overhead condenser temperature control is 100 DEG C, the temperature of cold-trap 2
10 DEG C are controlled to, the liquid phase hydrocarbon product for respectively obtaining carries out chromatogram off-line analysis.Now, in hot trap 1 during product chromatography
Between be 78 minutes, and product focuses primarily upon C in cold-trap 25～C18Vapour, diesel oil distillate section, the chromatography time is 60 minutes, color
Spectrogram is as shown in figure 3, data result is as shown in table 1.
【Embodiment 3】
Using Fischer-Tropsch synthesis condition same as Example 1, simply change catalyst and cause hydrocarbon product quality point
Cloth is：C1 =16.1%, C2～C4=10.2%, C5～C11=61.0%, C12～C17 =11.3%, C18～C27 =1.4%, C28 +
=0。
The bottom of towe heter temperature of hot trap 1 is set to into 250 DEG C, overhead condenser temperature control is 80 DEG C, the temperature control of cold-trap 2
10 DEG C are made as, the liquid phase hydrocarbon product for respectively obtaining carries out chromatogram off-line analysis.Now, the product chromatography time in hot trap 1
For 78 minutes, and product focused primarily upon C in cold-trap 25～C18Vapour, diesel oil distillate section, the chromatography time is about 40 minutes, color
Spectrogram is as shown in figure 4, data result is as shown in table 1.
【Embodiment 4】
Using catalyst same as Example 1, reaction condition and hydrocarbon product Mass Distribution, simply by the bottom of towe of hot trap 1
Heter temperature is set to 300 DEG C, in charging bottom, about 5 centimeter length stainless steel metal wires is filled about at the position of tower 2/3rds
Net to increase the contact area between the steam of rising and the liquid of decline, so as to strengthen the mass transfer between air-liquid, overhead condenser temperature
Degree is controlled to 50 DEG C.The temperature control of cold-trap 2 is 0 DEG C, and the liquid phase hydrocarbon product for respectively obtaining carries out chromatogram off-line analysis.Now,
C in hot trap 15～C11Gasoline fraction is reduced, C12 +Long chain hydrocarbons increase, and the chromatography time is 78 minutes, and product master in cold-trap 2
To be C5～C11Gasoline fraction, the chromatography time is about 30 minutes, and chromatogram is as shown in figure 5, data result is as shown in table 1.
【Embodiment 5】
Using catalyst same as Example 1, reaction condition and hydrocarbon product Mass Distribution, simply by the bottom of towe of hot trap 1
Heter temperature is set to 350 DEG C, and overhead condenser temperature control is 50 DEG C.The temperature control of cold-trap 2 is -5 DEG C.Respectively obtain
Liquid phase hydrocarbon product carries out chromatogram off-line analysis.Now, C in hot trap 15～C11Gasoline fraction is reduced, C12 +Long chain hydrocarbons increase, color
The analysis of spectrum time is 78 minutes, and product is mainly C in cold-trap 25～C11Gasoline fraction, the chromatography time is 30 minutes, color
Spectrogram as shown in fig. 6, data result as shown in table 1, by table 1 and with 93#、97#Gasoline chromatogram Fig. 7, Fig. 8 is compared, cold-trap 2
In the gasoline fraction that obtains be close to commercial gasoline carbon number distribution.
【Embodiment 6】
Using catalyst same as Example 1, reaction condition and hydrocarbon product Mass Distribution, simply by the bottom of towe of hot trap 1
Heter temperature is set to 380 DEG C, and overhead condenser is not opened, and adopts temperature for 25 DEG C of atmospheric condensation mode.The temperature of cold-trap 2
- 10 DEG C are controlled to, the liquid phase hydrocarbon product for respectively obtaining carries out chromatogram off-line analysis.Now, C in hot trap 15～C11Gasoline fraction
Further reduce, C12 +Long chain hydrocarbons, particularly C18 +Heavy hydrocarbon increases, and the chromatography time is 78 minutes, and product master in cold-trap 2
To be C5～C11Gasoline fraction, the chromatography time is 30 minutes, and chromatogram is as shown in figure 9, data result as shown in table 1, leads to
Cross table 1 and with 93#、97#Gasoline chromatogram Fig. 7, Fig. 8 is compared, the gasoline fraction obtained in cold-trap 2 and commercial gasoline carbon number distribution
It is close to.
【Comparative example 1】
Using catalyst same as Example 1, reaction condition and hydrocarbon product Mass Distribution, hot trap 1 is only as product
Holding vessel, tower bottom heater temperature control is 150 DEG C, and top of tower condenser temperature is controlled to 150 DEG C, no-arbitrary pricing in tower,
The temperature control of cold-trap 2 is 10 DEG C.The hydrocarbon product chromatography time obtained in hot trap 1 and cold-trap 2 is respectively 78 minutes, chromatogram
Figure respectively as shown in Figure 10 and Figure 11, more disperse in cold-trap 2, and data result is as shown in table 1 by hydrocarbon product carbon number distribution.
【Comparative example 2】
Using catalyst same as Example 2, reaction condition and hydrocarbon product Mass Distribution, hot trap 1 is only as product
Holding vessel, tower bottom heater temperature control is 150 DEG C, and top of tower condenser temperature is controlled to 150 DEG C, no-arbitrary pricing in tower,
The temperature control of cold-trap 2 is 5 DEG C.The hydrocarbon product chromatography time obtained in hot trap 1 and hot trap 2 is respectively 78 minutes, cold-trap 2
Middle hydrocarbon product carbon number distribution is more disperseed, and data result is as shown in table 1.
Table 1
Continued 1
Claims (6)
1. a kind of separation method of fischer-tropsch reaction product, by the hydrocarbon product that fischer-tropsch reaction is obtained separator is passed through；Product Jing
Separator is obtained containing vapour, the hydro carbons of diesel oil and heavy hydrocarbons product after separating, and the separator includes hot trap tower and heater,
Heater is 120～400 DEG C in the bottom of hot trap tower, hot trap column bottom temperature control range, and hot trap tower top temperature control range is
25～150 DEG C；
The hydrocarbon product that the fischer-tropsch reaction is obtained by percentage to the quality, including following components：15.1～19.5% C1, 9.0
～12.4% C2～C4, 50.0～65.0% C5～C11, 10.5～12.9% C12～C17, 0.4～4.7% C18~
C27, 0～0.5% C28 +；
The charging aperture of hydrocarbon product is respectively mounted filler in the middle part of hot trap tower at charging aperture upper and lower position, respectively positioned at hot trap tower
At 1/3rd and 2/3rds；
The isolated hydro carbons containing vapour, diesel oil is entered in ensuing cold-trap holding vessel, gasoline or petrol and diesel oil hydrocarbon product
Collected in the holding vessel, the temperature controlling range of cold-trap holding vessel is -10～25 DEG C.
2. the separation method of fischer-tropsch reaction product according to claim 1, it is characterised in that separator also includes product
Condenser, condenser is on the top of hot trap tower.
3. the separation method of fischer-tropsch reaction product according to claim 1, it is characterised in that hydrocarbon product is through separating dress
After putting separation, the hydro carbons containing vapour, diesel oil that hot trap tower top is obtained is collected in ensuing cold-trap, obtains C5～C11Gasoline fraction
Or C5～C18Vapour, diesel oil mixed fraction.
4. the separation method of fischer-tropsch reaction product according to claim 1 and 2, it is characterised in that hot trap column bottom temperature control
Scope processed is 150～380 DEG C.
5. the separation method of fischer-tropsch reaction product according to claim 1 and 2, it is characterised in that hot trap tower top temperature control
Scope processed is 25～80 DEG C.
6. the separation method of fischer-tropsch reaction product according to claim 1, it is characterised in that the temperature control of cold-trap holding vessel
Scope processed is -5～l0 DEG C.
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